EP4279848A1 - Procédé et appareil de refroidissement d'un débit riche en co2 - Google Patents

Procédé et appareil de refroidissement d'un débit riche en co2 Download PDF

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Publication number
EP4279848A1
EP4279848A1 EP23163363.7A EP23163363A EP4279848A1 EP 4279848 A1 EP4279848 A1 EP 4279848A1 EP 23163363 A EP23163363 A EP 23163363A EP 4279848 A1 EP4279848 A1 EP 4279848A1
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EP
European Patent Office
Prior art keywords
flow
heat exchanger
fluid
rich
pressure
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
EP23163363.7A
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German (de)
English (en)
French (fr)
Inventor
Martin Raventos
Richard Dubettier-Grenier
Mathieu LECLERC
Thomas Morel
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Publication date
Application filed by Air Liquide SA, LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical Air Liquide SA
Publication of EP4279848A1 publication Critical patent/EP4279848A1/fr
Pending legal-status Critical Current

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
    • F25J3/067—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream separation of carbon dioxide
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0266—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of carbon dioxide
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • F25J1/0235—Heat exchange integration
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0027—Oxides of carbon, e.g. CO2
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
    • F25J1/0052—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
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    • F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
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    • F25J1/0204—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a single-component refrigerant [SCR] fluid in a closed vapor compression cycle as a single flow SCR cycle
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0211—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
    • F25J1/0212—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a single flow MCR cycle
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J1/0222—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using the cold stored in an external cryogenic component in an open refrigeration loop in combination with an intermediate heat exchange fluid between the cryogenic component and the fluid to be liquefied
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • F25J1/0235—Heat exchange integration
    • F25J1/0242—Waste heat recovery, e.g. from heat of compression
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
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    • F25J1/0262—Details of the cold heat exchange system
    • F25J1/0264—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams
    • F25J1/0265—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams comprising cores associated exclusively with the cooling of a refrigerant stream, e.g. for auto-refrigeration or economizer
    • F25J1/0268—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams comprising cores associated exclusively with the cooling of a refrigerant stream, e.g. for auto-refrigeration or economizer using a dedicated refrigeration means
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    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
    • F25J1/0285—Combination of different types of drivers mechanically coupled to the same refrigerant compressor, possibly split on multiple compressor casings
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/62—Liquefied natural gas [LNG]; Natural gas liquids [NGL]; Liquefied petroleum gas [LPG]
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/04—Recovery of liquid products
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/02—Separating impurities in general from the feed stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/40—Separating high boiling, i.e. less volatile components from air, e.g. CO2, hydrocarbons
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/80—Separating impurities from carbon dioxide, e.g. H2O or water-soluble contaminants
    • F25J2220/82—Separating low boiling, i.e. more volatile components, e.g. He, H2, CO, Air gases, CH4
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/60—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being (a mixture of) hydrocarbons
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/12—External refrigeration with liquid vaporising loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/14—External refrigeration with work-producing gas expansion loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/60—Closed external refrigeration cycle with single component refrigerant [SCR], e.g. C1-, C2- or C3-hydrocarbons
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • F25J2270/902—Details about the refrigeration cycle used, e.g. composition of refrigerant, arrangement of compressors or cascade, make up sources, use of reflux exchangers etc.
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • F25J2270/904—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by liquid or gaseous cryogen in an open loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/34—Details about subcooling of liquids
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2

Definitions

  • the present invention relates to a method and an apparatus for cooling a flow rich in CO2.
  • At least part of the frigories required for cooling, or even liquefaction are provided by the heating of a fluid rich in methane, for example the vaporization of a liquid rich in methane, for example containing at least 80 mol% of methane. or the pseudo-vaporization of a methane-rich fluid in a dense phase.
  • a fluid is liquefied natural gas (LNG).
  • LNG liquefied natural gas
  • the transfer of frigories is carried out by using an intermediate fluid rich in ethane or ethylene to transfer the frigories of the liquefied gas, for example from liquefied natural gas to the liquefaction of the CO2-rich flow.
  • a flow rich in CO2 comprises at least 70 mol% carbon dioxide, preferably at least 90 mol% carbon dioxide, or even at least 95% carbon dioxide.
  • Liquefaction of a carbon dioxide-rich flow typically consumes electricity to provide the required refrigeration.
  • Liquefied natural gas is often vaporized against seawater or another calorigen.
  • the two systems have complementary needs, because the vaporization of liquefied natural gas requires heat and the liquefaction of carbon dioxide requires a cold source. It is therefore interesting to investigate the possibility of integrating the two systems.
  • the disadvantage of option a) is the incompatibility between the enthalpy-temperature profiles of the condensing CO2 and the intermediate fluid in the heat exchanger (most of the heat is produced by the CO2 at constant temperature while the temperature of the intermediate fluid increases at a constant rate, depending on its flow rate and its specific heat).
  • This obstacle can be avoided, for example, by increasing the flow rate of the intermediate fluid and/or by increasing the pressure of the CO2 to approach the critical pressure, or even exceed it. Both solutions require increasing energy and therefore these solutions are less attractive.
  • JPH04-131688 describes a closed intermediate fluid cycle that transfers cold from an LNG flow to a CO2 flow to be liquefied, the cycle including a pump to pressurize the intermediate fluid.
  • the fluid used is Freon® .
  • FR2869404 describes a closed intermediate fluid cycle that transfers cold from an LNG flow to a CO2 flow to be liquefied, the intermediate fluid being ethane that vaporizes against the CO2 and liquefies against the LNG.
  • the pressure of the intermediate fluid is constant.
  • the present invention aims to improve known processes by reducing the risk of freezing carbon dioxide in the cooling process, or even liquefaction of carbon dioxide.
  • This fluid uses an intermediate fluid to recover the cold from the LNG composed mainly of ethane and/or ethylene, which may also include methane.
  • This fluid will be designated as fluid C2.
  • This fluid preferably contains at least 90 mol% of ethane or ethylene.
  • This intermediate fluid preferably allows cold recovery down to temperatures below -60°C.
  • a dedicated heat exchanger (called an “LNG exchanger”) is used to exchange heat between the intermediate fluid and the methane-rich liquid, for example LNG liquefied natural gas in liquid form or in dense phase.
  • the LNG is heated or vaporized (depending on its pressure) against the condensing fluid C2 and is cooled to a temperature below -50°C in a single pass or in multiple parallel passes operating at different pressures (Pc1, Pc2 , PcN, where N is typically between 2 and 4), in order to limit temperature differences between exchanger fluids.
  • the LNG exchanger will typically be a brazed aluminum or stainless steel plate and fin exchanger, a shell and tube exchanger or a printed circuit exchanger.
  • the C2 fluid flows are preferably subcooled to a temperature between 2-10 K above the LNG inlet temperature into the exchanger.
  • all the subcooled C2 fluids are mixed at a pressure P1, possibly using at least one pump and reheated in another passage of the same exchanger to a temperature between 2 and 5K below of the bubble temperature of the mixed flows at pressure P1.
  • Subcooling the C2 fluid around -60°C is only a way of limiting temperature differences in the exchanger.
  • the vaporized fluid C2 to P1 (or the vaporized fluids at P1 and P2) obtained at the hot end of the heat exchanger where the CO2 condenses must be designed to produce the required flow rates at the chosen condensation pressures Pc1, Pc2, PcN for the LNG heating exchanger.
  • N currents at pressure values Pc1, Pc2, PcN and with specified flow rates. This supposes compressing at least one current and/or relaxing at least one current. It is important to exploit the pressure of the original streams (i.e., minimizing compression, particularly if it cannot be driven by the expansion of another stream in a turbine).
  • the number of flow rates of C2 fluid at different pressure passing through the LNG reheating exchanger is chosen according to the composition of the C2 fluid and the type of exchanger used. In general terms, the higher the number of flow rates, the smaller the temperature differences between the fluids, so reheating can for example be produced in a brazed aluminum plate and fin exchanger.
  • JP H04 121573A describe a method according to the preamble of claim 1.
  • An aim of the present invention is to limit temperature differences at the cold end of one of the exchangers, in order to increase the efficiency of the process.
  • the heat exchanger E2 two flows C2, here of ethane, 19, 21 are cooled, the flow 21 being at lower pressure than the flow 19.
  • the flow 21 passes through the heat exchanger E1 from the hot end to the cold end while condensing completely.
  • the condensed flow is sent into a tank S.
  • the liquid 23 of the tank S is pressurized by a pump P and mixed with the flow 19 which has condensed and which is expanded in a valve.
  • the flow formed 11 is de-cooled and therefore heated in the heat exchanger E1 to an intermediate temperature thereof, that is to say a temperature between that of the cold end and the hot end of the exchanger.
  • the flow 11 is sent to the CO2 liquefier either in a thermally insulated pipe or by passing through a thermally insulated cold box common to the E2 exchanger and the CO2 liquefier.
  • the flow 11 is divided in two and the two parts 13, 15 are expanded in respective valves and reheated in a heat exchanger E1 passing from the cold end to the hot end. After reheating, the flow 15 is divided in two to form the flow rates 19, 17.
  • the flow 19 is compressed in a compressor C, cooled in a cooler (not shown) and sent to the outlet pressure thereof at the exchanger E2.
  • Flow 17 is expanded from pressure P1 in a turbine T which drives compressor C and is mixed with flow 13 to form flow 21 which enters exchanger E2.
  • Reboiling of column K1 is provided by taking a portion 57 of the bottom liquid 55 of column K1 enriched with carbon dioxide.
  • the tank liquid 55 is sent to an intermediate level of the exchanger E1 hotter than the outlet point of the flow 51.
  • the part 57 is vaporized and reheated and returned to the tank of the column K1 as gas.
  • the remainder 7 of the liquid 55 is subcooled in the heat exchanger E1 by heat exchange with the intermediate fluid 11 and forms liquid carbon dioxide which is the product of the process.
  • the overhead gas 9 of column K1 heats up in the exchanger E1 from the cold end to the hot end and leaves the system. This gas 9 is enriched in light impurities such as nitrogen, hydrogen, carbon monoxide, etc.
  • the condensation pressure of the flow 19 of intermediate fluid in the second heat exchanger E2 is higher, preferably by at least 2 bars, than the highest vaporization pressure of the intermediate fluid in the first heat exchanger E1.
  • the fluid C2 vaporizes at two different pressures in the exchanger E2 to condense the gas rich in carbon dioxide.
  • the gas 15 taken from the hot end of the exchanger E1 is divided in two. A portion 45 is compressed in the compressor, cooled in a heat exchanger E3 and then condensed in the heat exchanger E2 against the LNG. The remainder 25 of the gas 15 is divided into three, a part 29 being mixed with the gas 13 to form a gas 43 which is expanded in the turbine driving the compressor and then is sent to the exchanger E2 to condense completely forming the liquid flow 47 sent to the S ball.
  • Another part 27 of the gas 25 is expanded then sent to the heat exchanger E2 where it is condensed and subcooled, then mixed with the subcooled liquid 47.
  • Another part 41 of the gas 25 is expanded then sent to the heat exchanger E2 where it is condensed and subcooled then mixed with liquid 47.
  • the exchanger E2 can be a plate and fin exchanger, for example in brazed aluminum since there is a cooler downstream of the compression of the flow 45.
  • the turbine is powered by the flow of fluid C2 here ethylene at pressure P2.
  • Exchanger E3 is cooled by means of a flow rate 1A of vaporized LNG taken from the hot outlet of exchanger E2.
  • the condensation pressure of the flow 45 of intermediate fluid in the second heat exchanger is higher, preferably at least 2 bars, than the highest vaporization pressure of the intermediate fluid in the first heat exchanger.
  • Exchanger E3 is cooled by means of a flow rate 1A of vaporized LNG taken from the hot outlet of exchanger E2.
  • the condensation pressure of the flow 33 of intermediate fluid in the second heat exchanger is higher, preferably by at least 2 bars, than the highest vaporization pressure of the intermediate fluid in the first heat exchanger.
  • FIG.4 represents a process for condensing CO2 by heat exchange with a liquid rich in methane, for example LNG, using a cycle in which the fluid is 93 mol% ethylene and 7 mol% methane with a single flow of condensing fluid in the exchanger E2
  • a flow of liquefied natural gas (LNG) 1 is sent to the cold end of a heat exchanger E2 which can be a plate and fin exchanger or a printed circuit exchanger.
  • the liquefied natural gas vaporizes and heats up in the exchanger E2 to produce natural gas 3 leaving the hot end preferably at a temperature above 0°C, for example ambient temperature.
  • Flow 11 is sent to the CO2 liquefier either in an insulated pipe or by passing through an insulated cold box common to the exchanger E2 and the CO2 liquefier.
  • Flow 11 becomes flow 13 and is reheated in a heat exchanger E1 passing from the cold end to the hot end. After reheating, the flow 13 is reheated again, for example up to 60°C, and sent at the outlet pressure of the heater R to the exchanger E2. The flow enters exchanger E2.
  • a flow 12 short-circuits the exchanger E1 to allow the intermediate fluid to be heated by a heater.
  • the flow 5 rich in carbon dioxide at between 10-16 bara is divided into two parts 51, 53
  • the flow 53 travels entirely through the exchanger E1 and is sent as reflux to the top of a distillation column K1, having condensed in the E1 exchanger.
  • the other part 51 cools in the exchanger E1 at the same pressure as the part 53 but leaves the exchanger E1 at an intermediate temperature between those of the hot end and the cold end. Part 51 is then sent to column K1.
  • Reboiling of column K1 is provided by taking a portion 57 of the bottom liquid 55 of column K1 enriched with carbon dioxide.
  • the tank liquid 55 is sent to an intermediate level of the exchanger E21 hotter than the outlet point of the flow 51.
  • the part 57 is vaporized and reheated and returned to the tank of the column K1 as gas.
  • the remainder 7 of the liquid 55 is subcooled in the heat exchanger E1 by heat exchange with the intermediate fluid 11 and forms liquid carbon dioxide which is the product of the process.
  • the overhead gas 9 of column K1 heats up in the exchanger E1 from the cold end to the hot end and leaves the system. This gas 9 is enriched in light impurities such as nitrogen, hydrogen, carbon monoxide, etc.
  • the condensation pressure of the flow 19 of intermediate fluid in the second heat exchanger only differs from the highest vaporization pressure of the intermediate fluid in the first heat exchanger by the pressure losses.
  • the intermediate fluid cycle does not include compression (apart from pressurization of the pump) nor expansion in a turbine. Pump P is only used to compensate for pressure losses.
  • THE [ FIG. 1 ], [ FIG. 2 ], [ FIG. 3 ] And [ FIG.4 ] respectively may comprise a pipe for bringing gas produced in the tank S upstream of the exchanger E2. This gas results from heat entering the balloon S, which vaporizes a small part of the liquid it contains. The gas formed 25 is sent from the balloon S and joins the gas 21.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Carbon And Carbon Compounds (AREA)
EP23163363.7A 2022-05-20 2023-03-22 Procédé et appareil de refroidissement d'un débit riche en co2 Pending EP4279848A1 (fr)

Applications Claiming Priority (1)

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FR2204833A FR3128011B1 (fr) 2022-05-20 2022-05-20 Procédé et appareil de refroidissement d’un débit riche en CO2

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EP4279848A1 true EP4279848A1 (fr) 2023-11-22

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US (1) US20230375266A1 (ja)
EP (1) EP4279848A1 (ja)
JP (1) JP2023171261A (ja)
KR (1) KR20230162547A (ja)
CN (1) CN117091352A (ja)
FR (1) FR3128011B1 (ja)

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5520206A (en) * 1978-07-24 1980-02-13 Showa Tansan Kk Manufacture of saturated liquefied carbon dioxide
JPH04121573A (ja) 1990-09-11 1992-04-22 Mitsubishi Heavy Ind Ltd Ｃｏ↓２ガスの液化方法
JPH08311438A (ja) * 1995-05-18 1996-11-26 Osaka Gas Co Ltd 液化炭酸製造用冷媒および液化炭酸製造設備の運転方法
JP2004069215A (ja) 2002-08-08 2004-03-04 Nippon Sanso Corp 熱交換装置及びその制御方法並びに液化天然ガスの冷熱を利用した炭酸ガスの液化方法
FR2869404A1 (fr) 2004-04-27 2005-10-28 Inst Francais Du Petrole Procede de liquefaction du dioxyde de carbone gazeux.
CN105545390A (zh) 2016-01-25 2016-05-04 辽宁石油化工大学 一种lng冷能梯级利用方法
FR3099234A1 (fr) * 2019-07-26 2021-01-29 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Procédé de récupération d’énergie frigorifique avec production d’électricité ou liquéfaction d’un courant gazeux

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5520206A (en) * 1978-07-24 1980-02-13 Showa Tansan Kk Manufacture of saturated liquefied carbon dioxide
JPH04121573A (ja) 1990-09-11 1992-04-22 Mitsubishi Heavy Ind Ltd Ｃｏ↓２ガスの液化方法
JPH08311438A (ja) * 1995-05-18 1996-11-26 Osaka Gas Co Ltd 液化炭酸製造用冷媒および液化炭酸製造設備の運転方法
JP2004069215A (ja) 2002-08-08 2004-03-04 Nippon Sanso Corp 熱交換装置及びその制御方法並びに液化天然ガスの冷熱を利用した炭酸ガスの液化方法
FR2869404A1 (fr) 2004-04-27 2005-10-28 Inst Francais Du Petrole Procede de liquefaction du dioxyde de carbone gazeux.
CN105545390A (zh) 2016-01-25 2016-05-04 辽宁石油化工大学 一种lng冷能梯级利用方法
FR3099234A1 (fr) * 2019-07-26 2021-01-29 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Procédé de récupération d’énergie frigorifique avec production d’électricité ou liquéfaction d’un courant gazeux

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JP2023171261A (ja) 2023-12-01
CN117091352A (zh) 2023-11-21
FR3128011B1 (fr) 2024-06-28
KR20230162547A (ko) 2023-11-28
FR3128011A1 (fr) 2023-04-14
US20230375266A1 (en) 2023-11-23

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